CN105073955B - Method and apparatus for heating hydrocarbon flow to process - Google Patents
Method and apparatus for heating hydrocarbon flow to process Download PDFInfo
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- CN105073955B CN105073955B CN201480018896.4A CN201480018896A CN105073955B CN 105073955 B CN105073955 B CN 105073955B CN 201480018896 A CN201480018896 A CN 201480018896A CN 105073955 B CN105073955 B CN 105073955B
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- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 97
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 96
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 94
- 238000000034 method Methods 0.000 title claims abstract description 78
- 238000010438 heat treatment Methods 0.000 title claims abstract description 61
- 230000008569 process Effects 0.000 title description 13
- 238000006243 chemical reaction Methods 0.000 claims abstract description 160
- 230000005855 radiation Effects 0.000 claims abstract description 46
- 239000002912 waste gas Substances 0.000 claims abstract description 29
- 238000012545 processing Methods 0.000 claims abstract description 21
- 239000002737 fuel gas Substances 0.000 claims abstract description 10
- 238000007600 charging Methods 0.000 claims description 25
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims description 18
- 239000001257 hydrogen Substances 0.000 claims description 18
- 238000012544 monitoring process Methods 0.000 claims description 11
- 230000035939 shock Effects 0.000 claims description 9
- 230000004044 response Effects 0.000 claims description 5
- 239000007789 gas Substances 0.000 claims description 4
- 239000003054 catalyst Substances 0.000 description 49
- 239000008187 granular material Substances 0.000 description 14
- 238000002407 reforming Methods 0.000 description 11
- 238000006057 reforming reaction Methods 0.000 description 11
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 8
- 230000008929 regeneration Effects 0.000 description 8
- 238000011069 regeneration method Methods 0.000 description 8
- 238000009835 boiling Methods 0.000 description 7
- 239000003502 gasoline Substances 0.000 description 7
- 238000012546 transfer Methods 0.000 description 7
- 238000001833 catalytic reforming Methods 0.000 description 6
- 230000008859 change Effects 0.000 description 6
- 238000006317 isomerization reaction Methods 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 238000011144 upstream manufacturing Methods 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 238000011027 product recovery Methods 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 150000001335 aliphatic alkanes Chemical class 0.000 description 4
- 150000001924 cycloalkanes Chemical class 0.000 description 4
- 238000006356 dehydrogenation reaction Methods 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- -1 alkyl cyclopentane Chemical compound 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 238000009826 distribution Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical group O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 229910052736 halogen Inorganic materials 0.000 description 2
- 150000002367 halogens Chemical class 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 230000008521 reorganization Effects 0.000 description 2
- NFGXHKASABOEEW-UHFFFAOYSA-N 1-methylethyl 11-methoxy-3,7,11-trimethyl-2,4-dodecadienoate Chemical compound COC(C)(C)CCCC(C)CC=CC(C)=CC(=O)OC(C)C NFGXHKASABOEEW-UHFFFAOYSA-N 0.000 description 1
- 229910052684 Cerium Inorganic materials 0.000 description 1
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 238000005899 aromatization reaction Methods 0.000 description 1
- 210000004556 brain Anatomy 0.000 description 1
- 150000001721 carbon Chemical group 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 125000001309 chloro group Chemical group Cl* 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 229910052732 germanium Inorganic materials 0.000 description 1
- GNPVGFCGXDBREM-UHFFFAOYSA-N germanium atom Chemical compound [Ge] GNPVGFCGXDBREM-UHFFFAOYSA-N 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- DMEGYFMYUHOHGS-UHFFFAOYSA-N heptamethylene Natural products C1CCCCCC1 DMEGYFMYUHOHGS-UHFFFAOYSA-N 0.000 description 1
- 125000004836 hexamethylene group Chemical group [H]C([H])([*:2])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[*:1] 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 229910052738 indium Inorganic materials 0.000 description 1
- APFVFJFRJDLVQX-UHFFFAOYSA-N indium atom Chemical compound [In] APFVFJFRJDLVQX-UHFFFAOYSA-N 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- 229910052741 iridium Inorganic materials 0.000 description 1
- GKOZUEZYRPOHIO-UHFFFAOYSA-N iridium atom Chemical compound [Ir] GKOZUEZYRPOHIO-UHFFFAOYSA-N 0.000 description 1
- 229910052747 lanthanoid Inorganic materials 0.000 description 1
- 150000002602 lanthanoids Chemical class 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- RGSFGYAAUTVSQA-UHFFFAOYSA-N pentamethylene Natural products C1CCCC1 RGSFGYAAUTVSQA-UHFFFAOYSA-N 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000009418 renovation Methods 0.000 description 1
- 238000012857 repacking Methods 0.000 description 1
- 230000003252 repetitive effect Effects 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G9/14—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils in pipes or coils with or without auxiliary means, e.g. digesters, soaking drums, expansion means
- C10G9/18—Apparatus
- C10G9/20—Tube furnaces
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Method and apparatus for processing hydrocarbon flow is provided.In one embodiment, the method for processing hydrocarbon flow heats including that will enter stream in convection bank.In the method, make to heat to form first effluent in the first reaction zone into stream.First effluent is heated in the first radiation pond, the first radiation pond makes fuel gas to be heated first effluent and form the first waste gas.This method includes making the first waste gas contact with convection bank will enter stream heating.
Description
Prioity claim
The U. S. application No.13/853 submitted this application claims on March 29th, 2013,802 priority will by quoting
During its content is fully incorporated herein.
Technical field
Technical field relates generally to the method and apparatus for processing hydrocarbon, more specifically it relates to in convection tube
Method and apparatus of the hydrocarbon to process is heated in beam.
Background
Hydroconversion process passes through series reaction area therein usually using hydrocarbon.Each reaction zone can have oneself uniqueness
Technological requirement, including required temperature.Therefore, each reaction zone is required in the enough heating amounts of the reaction zone upstream to realize at it
The required temperature that hydrocarbon needed for middle progress converts.
Hydroconversion process known to a kind of is catalytic reforming.Catalytic reforming is to enter in oil-refinery industry for improving hydrocarbon
The established hydroconversion process of the octane quality of material.The primary product of catalytic reforming is gasoline blending component or oil
The aromatic hydrocarbons source of product.Reformation may be defined as by cyclohexane dehydrogenation and alkyl cyclopentane and high-carbon content C6-C7Cycloalkane takes off
Hydrogen isomerization is to obtain aromatic hydrocarbons, paraffin dehydrogenation to obtain alkene, alkane and alkene dehydrocyclization to obtain aromatic hydrocarbons, normal paraffin
Hydrocarbon isomerization, alkyl-cycloalk hydrocarbon isomerization with obtain hexamethylene, substituted arene isomerization and alkane be hydrocracked caused by it is total
Effect.Catalytic reforming feedstock stream can be the product stream from hydrocracker, straight run, FCC or coker, and can include it is many its
Its component, such as condensate or thermal naphtha.
Heater or stove generally are used to heat process fluid before reaction in hydroconversion process such as reformation.It is general and
Speech, fired heater or stove include radiative flame heating zone to heat fluid, and wherein convection section is used for another service, such as produces
Steam.Each section includes pipe and flows through the process fluid of heater to accommodate.
In view of the fuel cost improved, conventional design meets with shortcoming.Specifically, it is not most to produce steam by convection section
Good, because steam provides in other regions of hydrocarbon processing devices.But carry out in comfortable radiative flame heating zone the combustion burnt
Heat content of the heat of material in hydrocarbon processing may be concentrated preferably when improving.
Accordingly, it is desirable to provide the method and apparatus for processing hydrocarbon of hydrocarbon flow is heated using convection section.In addition, reason
What is thought is the flow that convection section and the hydrocarbon flow of radiative flame heating zone are led in control.It is additionally desirable to provide economically grasp
This kind of method and apparatus made.In addition, other, preferably features and characteristics can be by subsequent detailed description and appended claims
Even if book in accompanying drawing and previous field and background together with learning.
General introduction
Method and apparatus for processing hydrocarbon flow is provided.In one embodiment, processing the method for hydrocarbon flow includes
Stream will be entered to heat in convection bank.In the method, make to react to form the first outflow in the first reaction zone into stream
Thing.First effluent is heated in the first radiation pond, the first radiation pond makes fuel gas with by first effluent
Heat and form the first waste gas.This method includes making the first waste gas contact with convection bank will enter stream heating.
In another embodiment, processing the method for hydrocarbon is included according to necessarily than hydrocarbon flow is divided into Part I and second
Part.Part I hydrocarbon flow is heated in convection bank.This method Part I hydrocarbon flow is reacted in the reaction region with
Form effluent.Part II hydrocarbon flow is added in effluent.This method includes heating effluent in pond is radiated, this shape
Into waste gas.Waste gas is set to be contacted with convection bank so that Part I hydrocarbon flow to be heated.In addition, method includes monitoring Part I hydrocarbon
The temperature of stream and adjusted when the temperature of Part I hydrocarbon flow exceedes maximum this than with change flow into convection bank in
The amount of Part I.
In another embodiment, there is provided the equipment for processing hydrocarbon flow.The equipment includes being configured to hydrocarbon flow
The heat exchanger of heating.Convection bank is configured to receive Part I hydrocarbon flow.In addition, reactor configurations be used for receive from pair
The Part I of flowing bundle simultaneously makes Part I react in the reaction region to form effluent.Equipment include be configured to receive and
Heat the radiation pond of effluent and Part II hydrocarbon flow.Radiation pond forms waste gas and is configured to make waste gas enter convection bank
In so that Part I hydrocarbon flow to be heated.In addition, equipment includes the temperature for being configured to the Part I that convection bank is left in monitoring
The temperature sensor of degree.The temperature that flow controller is configured to the Part I in response to leaving convection bank changes inflow pair
The amount of Part I in flowing bundle.
Brief description
The embodiment that the method and apparatus for processing hydrocarbon is described below along with the following drawings, wherein：
Fig. 1 is the signal of an embodiment of the method and apparatus for being used to heat hydrocarbon according to an embodiment to process
Figure；
Fig. 2 is the schematic diagram for illustrating the waste gas stream from the radiation area of Fig. 1 embodiment to convective region；With
Fig. 3 is the schematic diagram of the details of the convective region for the embodiment for illustrating Fig. 1.
It is described in detail
It is described in detail below merely illustrative in nature, and it is not intended to limit method or equipment for processing hydrocarbon.In addition,
It is not intended to any theoretical constraint by previous background or middle presentation described in detail below.
Provided herein is for processing hydrocarbon flow, more particularly, it is used to heat hydrocarbon flow in convection section in reaction zone upstream
Method and apparatus.This method and equipment reduce the fuel cost of radiative flame heating zone, because being carried as caused by fuel combustion
The energy of a large amount is transferred in hydrocarbon flow by convection section.As used herein, phrase " hydrocarbon flow " is included comprising various hydrocarbon molecules,
Such as straight chain, branched or cyclic alkane, alkene, alkadienes and alkynes and optional other mass, include gas such as hydrogen appoint
What stream.Hydrocarbon flow can be subjected to reacting, such as reforming reaction, but still referred to as hydrocarbon flow, and condition is that at least some hydrocarbon are reacting
It is present in later in the stream.Therefore, hydrocarbon flow may include the stream for being subjected to one or more reactions, such as hydrocarbon flow outflow
Thing, or any reaction is not subjected to, such as naphtha feed.As used herein, hydrocarbon flow may also include thick hydrocarbon (raw
Hydrocarbon stream, combined feed stream or effluent) are entered.
The method and apparatus as described herein for being used to heat hydrocarbon to process is especially suitable for the side using at least two reaction zone
Method, wherein at least a part of hydrocarbon flow flow serially through reaction zone.Method with multiple reaction zones may include that hydrocarbons convert
Method, such as reformation, hydrogenation, hydrotreating, dehydrogenation, isomerization, dehydrogenation-isomerization, dehydrocyclization, cracking and the side of being hydrocracked
Method.Catalytic reforming hereinafter refers to usually using multiple reaction zones described in figure in embodiment.However, lead
The method and apparatus opened is not limited to catalystic reforming method.
Accompanying drawing illustrates an embodiment for method and apparatus of the hydrocarbon processing as being applied to catalystic reforming method.Accompanying drawing
It is used merely to explain and presents and be not intended to limit the scope of claims as described below.Accompanying drawing only shows that understanding is each herein
Equipment and pipeline needed for embodiment, and do not show unnecessary for understanding method and apparatus claimed herein and be
Such as pump, compressor, heat exchanger and the valve of equipment known to technical staff in hydrocarbon manufacture field.
With reference to figure 1, the equipment 10 for processing hydrocarbon charging stream 12 is schematically described.Example apparatus 10 is to include heat exchange
Section 14, radiative flame bringing-up section 16, Convective Heating section 18, the reformer of conversion zone 20 and product recovery section 22.
As indicated, in the heat exchange segment 14 of the inflow segment 16,18 of hydrocarbon charging stream 12 and 20 upstreams.Example for catalytic reforming
Hydrocarbon charging stream 12 is the petroleum distillate of referred to as naphtha, and it has the initial boiling point of 82 DEG C (180 °F) and the end of 203 DEG C (400 °F)
Boiling point.Straight run stone brain of the catalystic reforming method especially suitable for handling the cycloalkane comprising larger concentration and basic linear paraffins
Oil, it is subjected to aromatisation by dehydrogenation and/or cyclization.The raw material of example is the ring substantially by that can be seethed with excitement in gasoline-range
The naphtha of alkane and alkane composition, but in many cases, aromatic hydrocarbons also may be present.This kind of naphtha include direct steaming gasoline,
Natural gasoline, synthetic gasoline etc..Other embodiments can load heat or catalytically cracked gasoline or partial conversion naphtha.Also may be used
Advantageously using straight run and the mixture of cracking gasoline range naphtha.Gasoline-range feed naphtha can be with 40-82
The initial boiling point of DEG C (104-180 °F) and the full boiling gasoline of the final boiling point of 160-220 DEG C (320-428 °F), or can be it
Selected cut, it is typically referred to as the high boiling fraction of heavy naphtha, such as boiling point is 100-200 DEG C of (212-
392 °F) naphtha.In some cases, additionally advantageously it is fitted into the alcohol hydrocarbon or hydrocarbon mixture reclaimed from extraction equipment, such as
Extract or linear paraffins from aromatic hydrocarbons extraction, it can change into aromatic hydrocarbons.In some other cases, enter stream 12 may be used also
Comprising the light hydrocarbon with 1-5 carbon atom, but because these light hydrocarbons are not easily formed aromatic hydrocarbons, generally make and enter stream 12 1
These light hydrocarbons entered are acted to minimize.
It is such as typical on catalystic reforming method, in the combined feed heat exchanger 30 being delivered in heat exchange segment 14 before
Stream 12 will be entered and mixed with the recycle stream 24 comprising hydrogen to form the stream of commonly referred to as combined feed stream 26.It is general and
Speech, recycle stream 24 feed the hydrogen of the amount of 1-20 every mole of hydrocarbon charging streams 12 of mol of hydrogen.For example, hydrogen can be fed to carry
For the amount less than every mole of hydrocarbon charging stream 12 of 3.5 mol of hydrogen.Provided that hydrogen, then it can be in combined feed heat exchanger 30
The upstream and downstream of upstream, the downstream of combined feed heat exchanger 30 or combined feed heat exchanger 30 provides.Or it can not provide
Hydrogen.Even if not supplying hydrogen gas into hydrocarbon charging stream 12, the cycloalkane reforming reaction carried out in conversion zone 20 can obtain hydrogen
As accessory substance.Hydrogen caused by the accessory substance or original position can obtain in the reaction zone downstream in conversion zone 20 as hydrogen.
Hydrogen in situ in conversion zone 20 can be to amount to 0.5-2 every mole of hydrocarbon charging streams 12 of mol of hydrogen.
In combined feed heat exchanger 30, combined feed stream 26 can pass through the exchanged heat of product effluent 36 with conversion zone 20
And heat.However, the heating of the combined feed stream 26 carried out in combined feed heat exchanger 30 is typically not enough to combined feed
Stream 26 is heated to the required inlet temperature of conversion zone 20.In typical catalystic reforming method, if hydrogen not with hydrocarbon charging stream
12 provide together, then combined feed stream 26 or hydrocarbon charging stream 12 are at usual 38-177 DEG C (100-350 °F), more generally 93-121 DEG C
Enter at a temperature of (200-250 °F) in combined feed heat exchanger 30.In general, combined feed heat exchanger 30 will be by that will come from
The product effluent 36 in last reforming reaction area is transferred in combined feed stream 26 and adds combined feed stream 26 in conversion zone 20
Heat.The combined feed heat exchanger 30 of example is valuable heavy in product effluent 36 to prevent for indirect rather than direct heat exchanger
Whole product mixes with combined feed stream 26, is thus recycled in conversion zone 20, wherein reforming amount of substance may deteriorate.
In another example embodiment, the stream of combined feed stream 26 and product effluent 36 in combined feed heat exchanger 30
Flowing mode is adverse current, although it can be complete cocurrent, reverse, mixing or cross-flow.In counter-current flow mode, combined feed
One end (cold end) of the heat exchange surface of combined feed heat exchanger 30, while product are contacted when stream 26 is at its most cold temperature
Effluent 36 also contacts the cold end of heat exchange surface at its most cold temperature.Therefore, product effluent 36 at it in heat exchanger
Most cold temperature under with the also combined feed stream exchanged heat at its most cold temperature in heat exchanger.In combined feed heat exchanger surface
The other end (i.e. hot junction), product effluent 36 and combined feed stream contact heat exchange in heat exchanger all at its most hot temperature
The hot junction on surface, thus exchanged heat.Between the h and c end of heat exchange surface, product effluent 36 and combined feed stream are with logical
Normal relative direction flowing so that in general, at any point along heat transfer surface, the temperature of product effluent 36 is hotter,
It is hotter with the temperature of the combined feed stream of the exchanged heat of product effluent 36.The combined feed heat exchanger 30 of example is to be typically smaller than 56
DEG C (100 °F), are, for example, less than 33 DEG C (60 °F), are, for example, less than the hot junction route operation of 28 DEG C (50 °F).
Although shell and tube exchanger can be used in combined feed heat exchanger 30, it is alternatively that, it may use that plate type heat exchanger.Plate
Formula exchanger is well known and commercially available in the form of several different and be unique, such as spiral, plate and frame, welding plate fin
(brazed-plate fin) and plate fin and tube type (plate fin-and-tube).
In one embodiment, combined feed stream 26 is used as hot feed at a temperature of 399-516 DEG C (750-960 °F)
Stream 40 leaves combined feed heat exchanger 30.Because the reforming reaction carried out first in reaction zone 60 is carried out at elevated temperatures
And it is usually what is absorbed heat, enters stream 40 and usually require that after combined feed heat exchanger 30 is left and in conversion zone 20 is entered
Heating in addition in the past.
In prior art device, the other heating is in such as the feed heater such as combustion gas, fuel oil of radiation pond or mixing combustion
There is provided in gas and fuel heater, it will enter stream 40 with convective heat transfer and heat by radiating or radiating.It is expected herein,
As needed, a part enters stream 40 and optionally bypasses any radiant heating area, but is heated in Convective Heating section 18
Without passing through pharoid.Therefore, Part I 44 enters the selectivity of stream 40 and is delivered in Convective Heating section 18.It is specific and
Speech, is controlled into stream 40 using valve 46 and is divided into Part I 44 and Part II 48.For example, valve 46 can be closed with by whole chargings
Stream 40 is sent into Convective Heating section 18 as Part I 44.When valve 46 is opened, the stream 40 of entering of selected amount is used as second
It is diverted into radiant heating section 16, while a certain amount of conduct Part I 44 is continued to flow into Convective Heating section 18.
In Convective Heating section 18, Part I 44 flows through Convective Heating tube bank 50, is such as further described on lower Fig. 2
's.Generally Part I 44 is heated to 482-560 DEG C (900-1,040 °F), such as 493-549 DEG C (920-1,020 °F)
Temperature.As indicated, Convective Heating stream 54 is left Convective Heating section 18 and flowed into conversion zone 20.Temperature indicator/controller
58 connect with the Convective Heating stream 54 of the upstream of conversion zone 20.In addition, temperature indicator/controller 58 and the electrical communication of valve 46.
Temperature indicator/controller 58 monitors the temperature of Convective Heating stream 54.When temperature exceedes predetermined maximum temp, such as 549 DEG C
When (1020 °F), the indication valve 46 of temperature indicator/controller 58 is closed to improve as Part I 44 and is delivered to Convective Heating
Section 18 in the percentage for entering stream 40, thus improve by Convective Heating restrain 50 Part I 44 flow velocity and reduce from
Open the temperature of the Convective Heating stream 54 of Convective Heating tube bank 50.Convective Heating is left when temperature indicator/controller 58 perceives
The temperature of the Convective Heating stream 54 of tube bank 50 is down to predetermined minimum temperature, for example, 546 DEG C (1015 °F) below when, temperature instruction
The indication valve 46 of device/controller 58 is opened to reduce as Part I 44 be delivered in Convective Heating section 18 enter stream 40 hundred
Fraction, thus reduce pair that Convective Heating tube bank 50 is left by the flow velocity and raising of the Part I 44 of Convective Heating tube bank 50
Flow the temperature of heats stream 54.
As indicated, Convective Heating stream 54 enters example conversion zone 20, the conversion zone 20 includes 4 that hydrocarbon flows in series over
Reaction zone 60.One kind in two kinds of forms is usually taken in conversion zone with multiple reaction zones 60：Stacking form as shown in Figure 1 or
Person's side-by-side fashion.In side-by-side fashion, the multiple and separated reaction vessels that can each include reaction zone can be put on side each other
Put.In stacking form, a common reaction vessel 62 is included in multiple and separated reaction zones 60 that top of one another is placed.
In each configuration, it is heat absorption or heat release depending on reacting, is heated or cooled between reaction zone 60 in the presence of centre.
The catalystic reforming method of example is used with the first reaction zone 71, second reaction zone 72, the 3rd reaction zone 73 and the
The conversion zone 20 of four reaction zones 74.Any number of reaction zone 60 may be present, but the number of reaction zone 60 is usually 3,4 or 5.Hydrocarbon
In each reaction zone 60 conversion reaction is undergone in the presence of catalyst granules 76.The reforming method of example is matched somebody with somebody in series flow
Catalyst granules 76 is used in the reaction zone 62 put, and spent catalyst particles 78 can leave conversion zone 20 as shown.
In terms of comprehensive, the first reaction zone 71 receives the Convective Heating stream 54 as first reactor charging and generation first
Effluent 81.The outlet temperature that the heat absorption reforming reaction carried out in the first reaction zone 71 typically results in the first reaction zone 71 is down to
The temperature of Convective Heating stream 54 is not only smaller than, and less than the required inlet temperature of second reaction zone 72.Therefore, will be first-class
Go out thing 81 to be heated to the required inlet temperature of second reaction zone 72 as described below in radiative flame bringing-up section 16 and be used as the
Two reactor feeds 82 are returned in conversion zone 20.Second reaction zone 72 makes the reaction of second reactor charging 82 form the second outflow
Thing 83.Further, since the endothermic reaction, second effluent 83 requires heating to reach the required inlet temperature of the 3rd reaction zone 73.
Second effluent 83 flows into and through radiative flame bringing-up section 16 as described below and heats and returned as the 3rd reactor feed 84
Return in conversion zone 20.3rd reaction zone 73 reacts the 3rd reactor feed 84 to form the 3rd reactor effluent 85.As above
Text, the endothermic reaction can cause the temperature of the 3rd reactor effluent 85 to be down to below the required inlet temperature of the 4th reaction zone 74.
3rd reactor effluent 85 flows into and is heated as described below by radiative flame bringing-up section 16 and be used as the 4th reactor feed
86 return in conversion zone 20.4th reaction zone 74 makes the 4th reactor feed 86 react to form product effluent 36.
Example reaction zone 60 can operate under the condition of reorganization, and the condition of reorganization is included generally from atmospheric pressure 0-6,
895kpag (0-1,000psig) pressure limit, wherein particularly preferred result is in 276-1,379kpag's (40-200psig)
Obtained under lower pressure scope.Total liquid hourly space velocity (LHSV) (LHSV) in all reaction zones is usually 0.1hr based on total catalyst volume-1
To 10hr-1, such as 1hr-1To 5hr-1, such as 1.5hr-1To 2.0hr-1。
In general, the cycloalkane reforming reaction of heat absorption is carried out in the first reaction zone 71, therefore the first reaction zone 71
Outlet temperature is smaller than the inlet temperature of the first reaction zone 71 and usually 316-454 DEG C (600-850 °F).First reaction zone 71
The usual 5-50%, more generally 10-30% of total catalyst volume in all reaction zones 60 can be included.Therefore, the first reaction zone 71
In liquid hourly space velocity (LHSV) (LHSV) based on the catalyst volume in the first reaction zone 71 can be usual 0.2-200hr-1, such as 2hr-1To 100hr-1, such as 5hr-1To 20hr-1.In general, catalyst granules is taken out from the first reaction zone 71 and into the
In two reaction zones 72.Particle is generally less than 2 weight % coke content with the weight based on catalyst.
The catalysis conversion method of example includes the catalyst granules 76 that may move through reaction zone 60.Catalyst granules 76 can
Reaction zone 60 is moved through by multi-motion device, including conveyer belt or trandfer fluid, but most generally, catalyst granules
76 can be moved through reaction zone 60 by gravity.Catalyst granules 76 can take out in the bottom by top reaction zone and introduce bottom
The top of reaction zone.The spent catalyst particles 78 taken out from final reaction zone then can be by reclaiming, in method again in method
Regenerate or be transferred in another reaction zone 60 in raw area's (not shown).Equally, the catalyst granules 76 added in reaction zone can
Think the catalyst that is regenerated in the catalyst in new Adding Way, the renewing zone in method or from another reaction zone 60
The catalyst of middle transfer.
The reforming reaction of example is generally carried out in the presence of catalyst granules 76, the catalyst granules include it is a kind of or
A variety of VIII (IUPAC 8-10) noble metals (such as platinum, iridium, rhodium and palladium) and with porous carrier such as refractory inorganic oxides knot
The halogen of conjunction.Although catalyst can include 0.05-2.0 weight %VIII races metal, relatively inexpensive catalyst can be used, such as wrap
The catalyst of the %VIII of weight containing 0.05-0.5 races metal.The noble metal of example is platinum.In addition, catalyst can include indium and/or
Lanthanide series metal such as cerium.Catalyst granules 76 can also include 0.05-0.5 weight % one or more IVA races (IUPAC 14) gold
Belong to (such as tin, germanium and lead).The halogen of example is chlorine, and the carrier of example is aluminum oxide.The alumina material of example is γ, η
With θ aluminum oxide, wherein γ and η aluminum oxide is generally used in selected embodiment.
Stationary catalyst bed or moving bed reaction container and moving bed regeneration container can be used in reforming method.In the latter
In, generally the catalyst granules 76 of regeneration is fed in the reaction vessel 62 for generally comprising several reaction zones 60, and catalyst particles
Grain 76 flows through reaction vessel 62 by gravity.During the reforming reaction process with moving catalyst bed, catalyst granules by
In various mechanism, for example, deposition of the coke on particle and become deactivation；I.e. after using certain time, catalyst granules promotees
Enter reforming reaction ability be down to catalyst there is no point.Before being used further in reforming method can by catalyst reparation or
Person regenerates.
Specifically, catalyst can be taken out and be delivered in regeneration container from the bottom of reaction vessel 62.Hold in regeneration
In device, multi-step renovation process is generally used for making catalyst regeneration recover whole abilities that it promotes reforming reaction.Catalyst
Each regeneration step can be flowed through by gravity, then takes out and is delivered in reaction vessel 62 from regeneration container.In general,
There is provided for adding fresh catalyst as the device for supplementing and taking out spent catalyst particles 78 from method.Catalyst moves
It is commonly referred to as continuous by reaction and regeneration container, although it is semi-continuous in practice.It is smaller in semicontinuous movement
The catalyst of amount is with close alternate interval repetitive displacement.For example, can with every 20 minutes by a collection of from the bottom of reaction vessel 62
5 minutes can be spent by taking out and taking out, i.e., catalyst can flow 5 minutes.If catalyst total amount and the batch in container
Compared to being larger, then it is believed that the catalyst bed in container is continuous moving.Mobile bed system, which can have, keeps yield, together
Shi Yidong or displacement catalyst the advantages of.Generally, catalyst be moved through catalyst bed speed can be and 45.5kg (100
Pound) the same as low as 2,722kg (6,000 pounds) is per hour or more per hour.
As shown in figure 1, in the downstream of the first reaction zone 71, radiation pond of the hydrocarbon in reaction zone 60 and radiative flame bringing-up section 16
Flowed between 90.For example, first effluent 81 leaves conversion zone 20 and if the amount for the Part II 48 for passing through valve 46 is more than 0
If mixed with the hot feed stream 40 of Part II 48.First effluent 81 (and Part II 48) and then the radiation of inflow first pond 91
In, it is heated there and forms second reactor charging 82.Second effluent 83 leaves conversion zone 20 and flows into the second spoke
Penetrate in pond 92, it is heated there and forms the 3rd reactor feed 84.Equally, third effluent 85 leaves conversion zone 20 simultaneously
Flow into the 3rd radiation pond 93, it is heated there and forms the 4th reactor feed 86.
Effluent stream between reaction zone and radiation pond generally can be with the flat Temperature Distribution on reaction zone entrance
Occur, i.e., hot effluent is identical temperature in all reaction zone porch.Or effluent stream can be with step temperature profile
Management.In each case, each radiation pond 90 (when it is between two reaction zones 60, commonly referred to as intermediate heater)
Burnt by the fuel gas 94 being optionally delivered to by valve 95 in radiation pond 90 to heat so that each effluent is heated into phase
Same temperature.
As in the first reaction zone 71, the endothermic reaction can cause another temperature on second reaction zone 72 to decline.However,
In general, the Wen Duxiajiang on second reaction zone 72 is less than the Wen Duxiajiang on the first reaction zone 71, because in the second reaction
Reaction less heat absorption of the reaction carried out in area 72 generally than being carried out in the first reaction zone 71.Although on second reaction zone 72 slightly
Micro- lower temperature declines, and second effluent 83 is still under the required inlet temperature lower temperature than the 3rd reaction zone 73.Cause
This, second effluent is heated to form the 3rd reactor feed 84 in the second radiation pond 92.
Second reaction zone 72 generally comprises the 10-60% of total catalyst volume in all reaction zones 60, more generally 15-
40%.Therefore, the liquid hourly space velocity (LHSV) (LHSV) in second reaction zone 72 is usually based on the catalyst volume in second reaction zone
0.13hr-1To 134hr-1, such as 1.3hr-1To 67hr-1, such as 3.3hr-1To 13.4hr-1。
In the 3rd reaction zone 73, the endothermic reaction can cause other Wen Duxiajiang, but it is typically smaller than the first reaction zone
Wen Duxiajiang on 71, because the reaction in the 3rd reaction zone 73 is typically less heat absorption.3rd reaction zone 73 includes all
The 25-75% of total catalyst volume, more generally 30-50% in reaction zone 60.For improve third effluent 85 temperature, by it
Heated in 3rd radiation pond 93.
In another example embodiment, each effluent 81,83 and 85 by U-tube enter and leave it is each radiation pond 91,
92 and 93 top.Or each effluent 81,83,85 can enter and leave the bottom in each radiation pond by inverted U pipe, or
It is to radiate minimum top in pond into temperature and is to radiate bottom most hot in pond to leave in temperature, or on the contrary, the bottom of into
Simultaneously left at top in portion.Certainly, although elaborating U-tube, many radiation ponds disk of the radiant heating available for effluent be present
Volume structure or design.
After being heated in the 3rd intermediate heater 93, the 4th reactor feed 86 is delivered in the 4th reaction zone 74.
4th reaction zone 74 includes the usual 30-80%, more generally 40-50% of total catalyst volume in all reaction zones 60.3rd,
Four and the inlet temperature in following reaction area be usually 482-560 DEG C (900-1,040 °F), such as 493-549 DEG C (920-1,020 °
F)。
Because the reforming reaction carried out in second and subsequent (i.e. third and fourth) reaction zone 60 is generally more anti-than first
Answer those carried out in area 71 are less to absorb heat, the temperature drop carried out in reaction zone 60 later is typically smaller than in the first reaction zone 71
Carry out.Therefore, the outlet temperature of final reaction zone 74 can be 11 DEG C (20 ° below the inlet temperature of final reaction zone 74
F it is) or smaller, it can essentially easily be higher than the inlet temperature of final reaction zone 74.In addition, the distribution of any inlet temperature can be with
Above-mentioned reaction zone 60 uses.Inlet temperature distribution can be flat or oblique, such as rise, decline, mountain type or paddy type.It is desirable that
The inlet temperature of reaction zone 60 is distributed as flat.
As indicated, product effluent 36 in combined feed heat exchanger 30 by contacting the heat to combined feed stream 26 and cold
But.After combined feed heat exchanger 30 is left, cold product effluent 96 enters in product recovery section 22.Suitable product recovery
Section 22 is well known.The product recovery section 22 of example may include gas-liquid separator with by hydrogen and C1-C3Appropriate hydrocarbon gas and production
Thing effluent 36 separates, and fractionating column is with by least a portion C4-C5Light hydrocarbon separates with remaining reformate.In addition, reformate
Light reformate cut and weight reformate cut can be separated by distillation into.Due to method for product recovery, formed product stream 98 or
Form the multiple product streams 98 for including required species.
Referring now to Figure 2, explain the heat transfer between radiative flame bringing-up section 16 and Convective Heating section 18.It is as indicated, each
Individual radiation pond 90 includes the radiant tube 102 with entrance 104 and outlet 106, and can be somewhat U-shaped and be upwardly oriented.
Although it illustrate only a radiant tube on each radiation pond 90, it should be understood that generally each radiation pond 90 may include entrance discrimination
Pipe, a series of pipes and outlet manifold.A series of radiant tubes 102 can be configured with parallel architecture and front and rear can stacked.Radiation
Pond 90 can be separated by fire division wall 112 and include at least one burner 122 respectively.
When effluent stream is by each corresponding radiation pond 90, fuel gas 94 burns in burner 122 and forms arrow
Flue gas shown in first 130.The flue gas 130 risen by radiating pond 90 can be added by one or more entrances 132 into convection current
Left in Convective Heating tube bank 50 in hot arc 18 and by chimney 134.Convective Heating tube bank 50 generally includes parallel architecture
Several convection tubes 138.Each convection tube 138 has entrance 142 and outlet 144 and can be somewhat U-shaped and oriented diagonally.
For multiple convection tubes 138, pipe 138 can be by stacking before and after row.Although convection tube 138 is orientated on side each other, it should be understood that
It is other orientation be it is possible, such as U-tube level land orientation and by row the several pipes 138 of vertical stacking.
Into Convective Heating section 18 a part 44 charging stream into convection tube 138 entrance 142 in and conveniently by
From the heat transfer of flue gas 130 by convection tube 138 and Convective Heating.Although entrance 142 is shown as making in outlet more than 144
Part 44 is top minimum in Convective Heating section 18 and is pair in temperature by oriented diagonally U-tube 138 into temperature
Most hot bottom is left in stream bringing-up section 18, it is contemplated that other configurations.For example, part 44 can enter and leave convection section 138
Top or bottom, or bottom enter and left at top.
Fig. 3 illustrates the Convective Heating tube bank 50 of example, and wherein convection tube 138 includes shock tube (shock tube) 152 Hes
Finned tube 154.Specifically, Convective Heating tube bank 50 is included in three row 156 shock tube of the finned tube of three row 158 below 154
152.The configuration can provide the more effective heat transfer for entering stream 40 to the part 44 for flowing through pipe 138 by uptake flue gas 130.
Specifically, the finned tube 154 in the colder part in 50 tops is restrained positioned at Convective Heating to be designed as being suitable to more effective heat transfer,
The shock tube 152 in the Convective Heating tube bank hotter part in 50 bottoms can better assure that hotter temperature simultaneously.
As described herein, there is provided apparatus and method of the heating hydrocarbon flow to be processed.In example embodiment, close
Apparatus and method are described in catalystic reforming method, but any suitable equipment and method for processing hydrocarbon are usable disclosed herein
Heating means.Although the embodiment above may be configured to new hydrocarbon processing equipment, it should be understood that disclosed feature can be
Performed during the repacking of existing equipment.
Although proposing at least one example embodiment in previous describe in detail, it is to be understood that a large amount of changes be present
Scheme.It should also be understood that one or more example embodiments are only example, and it is not intended to limit what is advocated in any way
Scope, application or the configuration of theme.But previously described in detail and be supplied to those skilled in the art to perform one or more examples
Embodiment facilitates route map.It should be understood that it can be made without departing from scope described in appended claims to example embodiment party
The function of element described in case and the various changes of configuration.
Specific embodiment
Although described hereafter together with specific embodiment, it should be understood that the description is intended to illustrate and do not limit preceding description
And the scope of the appended claims.
First embodiment of the invention is the method for processing hydrocarbon flow, be the described method comprises the following steps：Stream will be entered to exist
Heated in convection bank；Make to react to form first effluent in the first reaction zone into stream；By first effluent first
Radiation is heated in pond, wherein the first radiation pond makes fuel gas to be heated first effluent and form the first waste gas；With
The first waste gas is set to be contacted with convection bank so that stream heating will be entered.One embodiment of the invention is until the first implementation in this section
One in this section of scheme in previous example, it is any or all, it further comprises charging stream being divided into first
Point and Part II, wherein will enter stream heat in convection bank including by Part I enter stream in convection bank add
Heat, wherein making to react anti-first including making Part I enter stream to form first effluent in the first reaction zone into stream
Answer and reacted in area to form first effluent, and wherein method further comprises first effluent radiating Chi Zhongjia first
Part II is entered into stream before hot to mix with first effluent.One embodiment of the invention is until the first implementation in this section
One in this section of scheme in previous example, it is any or all, wherein charging stream is divided into Part I and second
Part includes the temperature for entering stream that convection bank is left in monitoring；With the temperature for entering stream in response to leaving convection bank, choosing
Improve to selecting property the amount that the Part I flowed into convection bank enters stream.One embodiment of the invention is until this Duan Zhong
One in this section of one embodiment in previous example, it is any or all, wherein the first reaction zone have it is required enter
Mouthful temperature and it will wherein feed that stream is divided into Part I and Part II includes the temperature for entering stream that monitoring leaves convection bank
Whether required inlet temperature is exceeded with temperature；And if temperature exceedes required inlet temperature, then optionally improve stream
Enter the amount that the Part I in convection bank enters stream.One embodiment of the invention is up to the first embodiment in this section
One in this section in previous example, it is any or all, wherein convection bank includes shock tube row (shock tube
Row) and/or finned tube arranges (finned tube row), and will wherein enter stream and be heated in convection bank including that will enter stream
Heated in shock tube row and/or in finned tube row.One embodiment of the invention is up to the first embodiment in this section
This section in one in previous example, it is any or all, it further comprises that stream will be being entered in convection bank
The circulating current comprising hydrogen is added into stream before heating.One embodiment of the invention is up to first is real in this section
Apply one in this section of scheme in previous example, it is any or all, it further comprises making first effluent
Reacted in two reaction zones to form second effluent；Second effluent is heated in the second radiation pond, wherein the second radiation pond
Make fuel gas to be heated second effluent and form the second waste gas；The second waste gas is set to be contacted with convection bank that will enter
Stream heats；Second effluent is set to be reacted in the 3rd reaction zone to form third effluent；By third effluent in the 3rd spoke
Penetrate in pond and heat, wherein the 3rd radiation pond makes fuel gas to be heated third effluent and form the 3rd waste gas；Make
Three waste gas are contacted with convection bank will enter stream heating；With third effluent is reacted in the 4th reaction zone to form product
Effluent.One embodiment of the invention is up to one in previous example in this section of the first embodiment in this section
Individual, any or all, it further comprises charging stream being divided into Part I and Part II, wherein will enter stream in convection current
Heating, which includes Part I entering stream in convection bank, in tube bank heats, wherein making to react in the first reaction zone into stream
Reacted with forming first effluent including making Part I enter stream in the first reaction zone to form first effluent, and wherein
Method further comprises Part II is entered into stream and the first outflow before first effluent is heated in the first radiation pond
Thing mixes.One embodiment of the invention is up to one in previous example in this section of the first embodiment in this section
Individual, any or all, it further comprises making product effluent pass through heat exchanger；With will enter stream in convection bank plus
It will enter stream before hot to heat in heat exchanger.One embodiment of the invention is up to the section of the first embodiment in this section
One in middle previous example, it is any or all, it further comprises condensing product effluent to form product stream.
One embodiment of the invention is one, Ren Hehuo until in this section in this section of the first embodiment in previous example
Person owns, and it further comprises charging stream being divided into Part I and Part II, adds wherein will enter stream in convection bank
Heat, which includes Part I entering stream in convection bank, to be heated, wherein making to react in the first reaction zone into stream to form the
One effluent is reacted to form first effluent including making Part I enter stream in the first reaction zone, and wherein method enters one
Step is included in first effluent is heated in the first radiation pond before Part II entered into stream mixed with first effluent.This
One embodiment of invention be until one in this section in this section of the first embodiment in previous example, it is any or
It is all, include monitoring the temperature for entering stream for leaving convection bank wherein stream will be fed and be divided into Part I and Part II；With
The temperature for entering stream in response to leaving convection bank, optionally improve the Part I flowed into convection bank and enter stream
Amount.One embodiment of the invention is, times until in this section in this section of the first embodiment in previous example
What is all, wherein the first reaction zone has required inlet temperature and charging stream wherein is divided into Part I and second
Dividing includes monitoring whether the temperature for entering stream for leaving convection bank exceedes required inlet temperature with temperature；If temperature surpasses
Required inlet temperature is crossed, then optionally improves the amount that the Part I flowed into convection bank enters stream.
Second embodiment of the invention is the method for processing hydrocarbon flow, be the described method comprises the following steps：According to certain
Than hydrocarbon flow is divided into Part I and Part II；Part I hydrocarbon flow is heated in convection bank；Make Part I
Hydrocarbon flow reacts to form effluent in the reaction region；Part II hydrocarbon flow is added in effluent；Effluent is being radiated
Heated in pond, wherein radiation pond forms waste gas；Waste gas is set to be contacted with convection bank so that Part I hydrocarbon flow to be heated；Monitoring the
The temperature of a part of hydrocarbon flow；With adjusted when the temperature of Part I hydrocarbon flow exceedes maximum this than with change flow into convection current
The amount of Part I in tube bank.One embodiment of the invention is until previously real in the section of the second embodiment in this section
Apply one in scheme, it is any or all, it further comprises making effluent react to form second in second reaction zone
Effluent；Second effluent is heated in the second radiation pond, wherein the second radiation pond forms the second waste gas；Make the second waste gas with
Convection bank is contacted so that Part I hydrocarbon flow to be heated；Second effluent is set to be reacted in the 3rd reaction zone to form the 3rd stream
Go out thing；Third effluent is heated in the 3rd radiation pond, wherein the 3rd radiation pond forms the 3rd waste gas；Make the 3rd waste gas with it is right
Flowing bundle is contacted so that Part I hydrocarbon flow to be heated；With third effluent is reacted in the 4th reaction zone to form product stream
Go out thing.One embodiment of the invention be until one in this section in this section of the second embodiment in previous example,
Any or all, it further comprises making product effluent pass through heat exchanger；With according to necessarily than hydrocarbon flow is divided into the
Hydrocarbon flow is heated in heat exchanger before a part and Part II.One embodiment of the invention is until second in this section
One in this section of embodiment in previous example, it is any or all, it further comprises product effluent is cold
Coagulate to form product stream.One embodiment of the invention is up to previous example in section of the second embodiment in this section
In one, it is any or all, its further comprise by Part II hydrocarbon flow add effluent in before make second
Divide hydrocarbon charging by valve, and wherein adjustment to change the amount of the Part I flowed into convection bank than including shutoff valve.This hair
A bright embodiment is up to one, any or institute in previous example in this section of the second embodiment in this section
Have, wherein the temperature of monitoring Part I hydrocarbon flow includes the temperature that the Part I hydrocarbon flow of convection bank is left in monitoring.
Third embodiment of the invention is the equipment for processing hydrocarbon flow, and the equipment includes being configured to heat hydrocarbon material
The heat exchanger of stream；It is configured to receive the convection bank of Part I hydrocarbon flow；It is configured to receive the from convection bank
A part simultaneously makes Part I react in the reaction region to form the reaction zone of effluent；It is configured to receive and heat effluent
With the radiation pond of Part II hydrocarbon flow, wherein radiation pond forms waste gas, and wherein radiation pond be configured to pass through waste gas it is right
Flowing bundle is to heat Part I hydrocarbon flow；It is configured to monitor the TEMP of the temperature for the Part I for leaving convection bank
Device；Change the Part I in inflow convection bank with the temperature for being configured to the Part I in response to leaving convection bank
The flow controller of amount.
It is not described any further, it is believed that previous description can be used in those skilled in the art, uses this most integrated degree
Invent and easily determine the essential characteristic of the present invention without departing from its spirit and scope, with make the various change of the present invention and
Improve and make it suitable for various uses and condition.Therefore, foregoing preferred embodiment is interpreted as being merely illustrative,
And the remainder of disclosure is not limited in any way, and be intended to cover be included in scope
Various improvement and equivalent arrangements.
Above, unless otherwise indicated, all temperature are with a DEG C description, all parts and percentage are by weight.
Claims (7)
1. processing the method for hydrocarbon flow, the described method comprises the following steps：
Charging stream is divided into Part I and Part II；
The Part I for entering stream is heated in convection bank；
The Part I into stream is set to be reacted in the first reaction zone to form first effluent；
Part II is mixed with first effluent；
First effluent and Part II are heated in the first radiation pond, wherein the first radiation pond makes fuel gas to incite somebody to action
First effluent heats and forms the first waste gas；With
The first waste gas is set to be contacted with convection bank so that stream heating will be entered.
2. method according to claim 1, wherein charging stream is divided into Part I and Part II includes：
The temperature for entering stream of convection bank is left in monitoring；With
The temperature for entering stream in response to leaving convection bank, optionally improve the Part I charging flowed into convection bank
The amount of stream.
3. method according to claim 1, wherein the first reaction zone has required inlet temperature and charging stream wherein is divided into the
A part and Part II include：
Whether the temperature for entering stream that convection bank is left in monitoring exceedes required inlet temperature with temperature；And
If temperature exceedes required inlet temperature, optionally improve the Part I flowed into convection bank and enter stream
Amount.
4. method according to claim 1, wherein convection bank include, shock tube is arranged and/or finned tube is arranged, and wherein will charging
Stream heating in convection bank includes entering stream and heated in shock tube row and/or in finned tube row.
5. method according to claim 1, it further comprises that hydrogen will be included before it will enter stream and heat in convection bank
The circulating current of gas is added into stream.
6. method according to claim 1, it further comprises：
After Part II is mixed with first effluent and heats first effluent and Part II in the first radiation pond,
First effluent is set to be reacted in second reaction zone to form second effluent；
Second effluent is heated in the second radiation pond, wherein the second radiation pond makes fuel gas with by second effluent
Heat and form the second waste gas；
The second waste gas is set to be contacted with convection bank so that stream heating will be entered；
Second effluent is set to be reacted in the 3rd reaction zone to form third effluent；
Third effluent is heated in the 3rd radiation pond, wherein the 3rd radiation pond makes fuel gas with by third effluent
Heat and form the 3rd waste gas；
The 3rd waste gas is set to be contacted with convection bank so that stream heating will be entered；With
Third effluent is set to be reacted in the 4th reaction zone to form product effluent.
7. method according to claim 6, it further comprises：
Product effluent is set to pass through heat exchanger；With
It will enter stream before it will enter stream and heat in convection bank to heat in heat exchanger.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US13/853,802 | 2013-03-29 | ||
| US13/853,802 US9206358B2 (en) | 2013-03-29 | 2013-03-29 | Methods and apparatuses for heating hydrocarbon streams for processing |
| PCT/US2014/031821 WO2014160750A1 (en) | 2013-03-29 | 2014-03-26 | Methods and apparatuses for heating hydrocarbon streams for processing |
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| Publication Number | Publication Date |
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| CN105073955A CN105073955A (en) | 2015-11-18 |
| CN105073955B true CN105073955B (en) | 2017-11-24 |
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| CN201480018896.4A Active CN105073955B (en) | 2013-03-29 | 2014-03-26 | Method and apparatus for heating hydrocarbon flow to process |
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| US (1) | US9206358B2 (en) |
| CN (1) | CN105073955B (en) |
| WO (1) | WO2014160750A1 (en) |
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| RU2685725C1 (en) * | 2016-05-13 | 2019-04-23 | Юоп Ллк | Reforming method with improved heater integration |
| EP3724298A1 (en) * | 2017-12-15 | 2020-10-21 | SABIC Global Technologies B.V. | Method for preheating naphtha in naphtha catalytic cracking processes |
| US11021657B2 (en) | 2018-04-26 | 2021-06-01 | Uop Llc | Process and apparatus for a convection charge heater having a recycle gas distributor |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4792436A (en) * | 1987-05-08 | 1988-12-20 | Kinetics Technology International | Hydrocarbon converter furnace |
| US5976354A (en) * | 1997-08-19 | 1999-11-02 | Shell Oil Company | Integrated lube oil hydrorefining process |
| CN1200914C (en) * | 1996-08-23 | 2005-05-11 | 环球油品公司 | Method for raising production ability by adopting reaction area shifted structure bypass |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3069351A (en) | 1959-07-17 | 1962-12-18 | Socony Mobil Oil Co Inc | Utilization of reformer make gas |
| US3069348A (en) | 1959-07-22 | 1962-12-18 | Socony Mobil Oil Co Inc | Multi-stage, multi-zone static bed reforming process and apparatus therefor |
| SU394410A1 (en) | 1970-01-13 | 1973-08-22 | MULTI FLOW TUBULAR FURNACE | |
| US5264202A (en) | 1990-11-01 | 1993-11-23 | Air Products And Chemicals, Inc. | Combined prereformer and convective heat transfer reformer |
| US7204966B2 (en) | 2002-11-08 | 2007-04-17 | Ashutosh Garg | Method and apparatus for improved fired heaters |
| US20080110801A1 (en) | 2006-11-09 | 2008-05-15 | Leon Yuan | Process For Heating A Hydrocarbon Stream Entering A Reaction Zone With A Heater Convection Section |
-
2013
- 2013-03-29 US US13/853,802 patent/US9206358B2/en active Active
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2014
- 2014-03-26 WO PCT/US2014/031821 patent/WO2014160750A1/en active Application Filing
- 2014-03-26 CN CN201480018896.4A patent/CN105073955B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4792436A (en) * | 1987-05-08 | 1988-12-20 | Kinetics Technology International | Hydrocarbon converter furnace |
| CN1200914C (en) * | 1996-08-23 | 2005-05-11 | 环球油品公司 | Method for raising production ability by adopting reaction area shifted structure bypass |
| US5976354A (en) * | 1997-08-19 | 1999-11-02 | Shell Oil Company | Integrated lube oil hydrorefining process |
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| WO2014160750A1 (en) | 2014-10-02 |
| US9206358B2 (en) | 2015-12-08 |
| CN105073955A (en) | 2015-11-18 |
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